CA2020307A1 - Process for soap splitting using a high temperature treatment - Google Patents
Process for soap splitting using a high temperature treatmentInfo
- Publication number
- CA2020307A1 CA2020307A1 CA002020307A CA2020307A CA2020307A1 CA 2020307 A1 CA2020307 A1 CA 2020307A1 CA 002020307 A CA002020307 A CA 002020307A CA 2020307 A CA2020307 A CA 2020307A CA 2020307 A1 CA2020307 A1 CA 2020307A1
- Authority
- CA
- Canada
- Prior art keywords
- soapstock
- high temperature
- splitting
- acid
- minutes
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
- 238000000034 method Methods 0.000 title claims abstract description 23
- 238000011282 treatment Methods 0.000 title claims abstract description 21
- 239000000344 soap Substances 0.000 title claims abstract description 18
- 239000002253 acid Substances 0.000 claims abstract description 28
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 239000000203 mixture Substances 0.000 claims abstract description 8
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 3
- 238000002156 mixing Methods 0.000 claims abstract description 3
- 206010037660 Pyrexia Diseases 0.000 claims 1
- 239000003921 oil Substances 0.000 description 14
- 235000019198 oils Nutrition 0.000 description 14
- 239000012071 phase Substances 0.000 description 11
- 239000000839 emulsion Substances 0.000 description 8
- 125000005456 glyceride group Chemical group 0.000 description 7
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- 239000001117 sulphuric acid Substances 0.000 description 6
- 235000011149 sulphuric acid Nutrition 0.000 description 6
- 239000000463 material Substances 0.000 description 5
- 235000005687 corn oil Nutrition 0.000 description 4
- 235000021588 free fatty acids Nutrition 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 235000019486 Sunflower oil Nutrition 0.000 description 3
- 235000014113 dietary fatty acids Nutrition 0.000 description 3
- 239000000194 fatty acid Substances 0.000 description 3
- 229930195729 fatty acid Natural products 0.000 description 3
- 150000004665 fatty acids Chemical class 0.000 description 3
- 239000002600 sunflower oil Substances 0.000 description 3
- UFTFJSFQGQCHQW-UHFFFAOYSA-N triformin Chemical compound O=COCC(OC=O)COC=O UFTFJSFQGQCHQW-UHFFFAOYSA-N 0.000 description 3
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- 241000208818 Helianthus Species 0.000 description 2
- 235000003222 Helianthus annuus Nutrition 0.000 description 2
- 239000008346 aqueous phase Substances 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000010924 continuous production Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 229910017053 inorganic salt Inorganic materials 0.000 description 2
- 238000007127 saponification reaction Methods 0.000 description 2
- 125000001273 sulfonato group Chemical class [O-]S(*)(=O)=O 0.000 description 2
- 238000010977 unit operation Methods 0.000 description 2
- 102000004895 Lipoproteins Human genes 0.000 description 1
- 108090001030 Lipoproteins Proteins 0.000 description 1
- 244000046052 Phaseolus vulgaris Species 0.000 description 1
- 235000010627 Phaseolus vulgaris Nutrition 0.000 description 1
- 235000019484 Rapeseed oil Nutrition 0.000 description 1
- 235000019485 Safflower oil Nutrition 0.000 description 1
- 240000008042 Zea mays Species 0.000 description 1
- 235000016383 Zea mays subsp huehuetenangensis Nutrition 0.000 description 1
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 238000009874 alkali refining Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 238000004040 coloring Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 235000012343 cottonseed oil Nutrition 0.000 description 1
- 239000002385 cottonseed oil Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 150000007529 inorganic bases Chemical class 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 235000009973 maize Nutrition 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 235000005713 safflower oil Nutrition 0.000 description 1
- 239000003813 safflower oil Substances 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 235000012424 soybean oil Nutrition 0.000 description 1
- 239000003549 soybean oil Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 235000021122 unsaturated fatty acids Nutrition 0.000 description 1
- 150000004670 unsaturated fatty acids Chemical class 0.000 description 1
- 235000013311 vegetables Nutrition 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B13/00—Recovery of fats, fatty oils or fatty acids from waste materials
- C11B13/02—Recovery of fats, fatty oils or fatty acids from waste materials from soap stock
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/74—Recovery of fats, fatty oils, fatty acids or other fatty substances, e.g. lanolin or waxes
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Wood Science & Technology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Detergent Compositions (AREA)
- Fats And Perfumes (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Processing Of Solid Wastes (AREA)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
- Edible Oils And Fats (AREA)
Abstract
P HP/LS/Uni-55 ABSTRACT
The invention relates to a process for splitting soapstock, comprising the steps of mixing the soapstock with a soap splitting acid, and of separating the acid water phase formed from the oil phase, characterized in that the mixture of the soapstock and the soap splitting agent are subjected to a high temperature treatment at or above 100°C
during a residence time equal to or more than 2 minutes.
*****
The invention relates to a process for splitting soapstock, comprising the steps of mixing the soapstock with a soap splitting acid, and of separating the acid water phase formed from the oil phase, characterized in that the mixture of the soapstock and the soap splitting agent are subjected to a high temperature treatment at or above 100°C
during a residence time equal to or more than 2 minutes.
*****
Description
P HP/L,S~Uni-55 2020~7 PROCESS FOR SOAP SPLITTING USING
~ HIGH TEMPERATURE TREATMENT
________________________________ The present invention relates to a process for split-ting soapstock, comprising the steps of mixing the soapstock with a soap splitting acid, and of separating the acid water phase formed from the oil phase.
Glyceride oils of in particular vegetable origin, such as maize oil, sunflower oil, soybean oil, rapeseed oil, safflower oil, cotton seed oil and the like, are valuable raw materials for the food industries. These oils in crude form are usually obtained from seeds and beans by pressing and/or solvent extraction.
Such crude glycerlde oils mainly conslst of triglyce-ride components. However, they generally also contain a signlflcant amount of non-triglyceride components including phosphatldes (gums~, waxy substances, partial glycerides, free fatty acids, sterolglucosidesand esters thereof, sucrolipids, lipoproteins, colouring materials and small amounts of metals. Dependlng on the intended use of the oil, many of these impurities have an undesirable effect on the (storage) stablllty, taste, and colour of later products. It ls therefore necessary to reflne, l.e. to remove the gums and other components from the crude glyceride oils as much as possible.
In general the flrst step in the refining of glyceride oils is the so-called degumming step, i.e. the removal of the phosphatides. In a conventional degumming process water is added to the crude gluceride oll to hydrate the phospha-tides, which are subsequently removed e.g. by centrifugal separation. Since the resulting degummed oil often still contains unacceptably high levels of 'non-hydratable' phos-phatldes, this water~degumming step is normally followed bychemical treatments with acid and/or alkali to remove the ~20307 residual phosphatides and to neutralize the free fatty acids (~alkali-refining~). Subsequently, the soapstock so formed is separated from the neutrali~ed oil by centrifugal separa-tion.
Soapstock containing the afore-mentioned non-triglyceride components and has to be split prior to it's disposal in order to recover the fatty acids contained therein, and to obtain an effluent (acid water) containing low levels of total fatty matter (TFM), that is material lo soluble in ether.
During the splitting of the soapstock using a soap splitting acid, such as sulphuric acid, at pH 2 and a soap splitting temperature of 95C, an emulsion may be formed.
The emulsion formation occurs especially when splitting maize- or sunflower soapstock.
There are several unit operations available to break the emulsions formed. These unlt operations comprise filtra-tion, centrifugation, settling during long time periods and a low pH treatment. All these unit operation are cumbersome, because of the corrosive nature of the emulsion (for instance a pH of 4 or lower), whereas due to the large amount of acid used the effluent may require a pre-treatment before disposal.
NL-A-69 17290 discloses a method and an apparatus for continuously splitting of soapstock formed in the alkall reflning of crude glyceride oil, in which an inorganic acld is lntensively mixed with steam ln a Venturl tube, and subsequently the acid steam mlxture is lntensively mlxed wlth soapstock ln a second Venturl tube. The soapstock had a temperature of 80-95C and was passed through a separatlon zone comprising a packed bed of filling material.
GB-A-1,307,862 discloses a process for treating a solutlon comprlslng soapstock, sulphonate salt and an lnorganlc salt for the recovery of fatty acid and a sulphonate salt solution therefrom. This mixture is acidified at 80C to pH 2,5 using sulphoric acid.
US-A-4,118,407 discloses a process for recovering free fatty acid from aqueous crude soapstock containing ~3~ 2020307 saponlfiable fatty material comprising a glyce~ide oil, comprising a saponification zone in which crude soapstock is mixed with an inorganic base and recycled inorganic salt containing neutralized acid water. The saponified soapstock is passed to a acidulation zone in which it is mixed with an inorganic salt at a temperature of between about 80-95C.
Finally, a free fatty acid stream is separated in a separation zone and neutralized acid water is recycled to the saponification zone.
US-A-4,671,902 discloses a method for the preparation of fatty acid products from glyceride oil soapstock, in which the soapstock is acidulated with an aqueous mineral acid, and after separation of an aqueous solution the remaining emulsion of fatty material and sludge is dried to a watter content of less than 5% resulting in a breakage of the emulsion. The acidiflcation is carried out at 80-95C, at a pH of 3-4, for at least two hours.
It has been found that when the mixture of soapstock and soap splitting agent is sub;ected to a high temperature treatment, the emulsion formation is substantially avoided.
Accordingly, an ob;ect of the invention is to provide a process for splitting soapstock, by which the emulsion formatlon is substantially avoided and accordingly, the acid water phase and oll phase formed are easily separatable from one another. The process of the invention is characterized in that the mixture of the soapstock and the soap splitting acid are sub~ected to a high temperature treatment at or above 100C during a residence tlme equal to or more than 2 minutes.
Preferably the high temperature treatment ls carried out at a temperature of about 100-150C. The upper temperature limit is elected such that the pressure is not too far above atmospheric pressure (pressure less than 6 bar).
Generally, a residence time of about 15-60 minutes is sufficient and optimal results are obtained after a resi-dence time of about 20-40 minutes.
-q- 2020307 Generally, the high temperature treatment is carried out at a pH of about 0~5-4, particularly at a pH near or equal to pTI 2.
Preferably, the splitted soapstock is settled at a temperature lower than the temperature of the high temperature treatment for separating the acid oil phase from the acid water phase. Preferably, the settling is carried out after cooling to a temperature of about 50-95C. A lower settling temperature is preferred, because at those lower temperatures the phase separation occurs within normally 15 minutes and the decrease of the solubility of the total fatty matter (TFM) in the acid water phase is larger than the increase of the viscosity of water.Finally, settling at the high temperature requires a pressure vessel, cooling of the acid water outlet and high investment costs for the pressure settling vessel and above all severe corrosion problems.
Generally, the high temperature treatment according to the invention leads to significantly lower TFM contents in the acid water phase, generally to TFM contents less than lO00 ppm.
Preferably, the soapstock originates from non-degummed or water-degummed glyceride oil.
The soap splitting process according to the invention may be used in a continuous process or in a batchwise process.
The following examples are given to illustrate the soap splitting process according to the invention, and may not be construed as to limit the invention described herein.
EXAMPLE I
Soapstock originating from non-degummed maize oil heated to a temperature of 95C was mixed with concentrated sulphuric acid untill pH 2 was reached. The mixture of soapstock and sulphuric acid was subjected to the high temperature treatment accordlng to the invention, using temperatures indicated in table l, and allowing a residence time of 2 minutes. The amount of TFM in the acid water phase was
~ HIGH TEMPERATURE TREATMENT
________________________________ The present invention relates to a process for split-ting soapstock, comprising the steps of mixing the soapstock with a soap splitting acid, and of separating the acid water phase formed from the oil phase.
Glyceride oils of in particular vegetable origin, such as maize oil, sunflower oil, soybean oil, rapeseed oil, safflower oil, cotton seed oil and the like, are valuable raw materials for the food industries. These oils in crude form are usually obtained from seeds and beans by pressing and/or solvent extraction.
Such crude glycerlde oils mainly conslst of triglyce-ride components. However, they generally also contain a signlflcant amount of non-triglyceride components including phosphatldes (gums~, waxy substances, partial glycerides, free fatty acids, sterolglucosidesand esters thereof, sucrolipids, lipoproteins, colouring materials and small amounts of metals. Dependlng on the intended use of the oil, many of these impurities have an undesirable effect on the (storage) stablllty, taste, and colour of later products. It ls therefore necessary to reflne, l.e. to remove the gums and other components from the crude glyceride oils as much as possible.
In general the flrst step in the refining of glyceride oils is the so-called degumming step, i.e. the removal of the phosphatides. In a conventional degumming process water is added to the crude gluceride oll to hydrate the phospha-tides, which are subsequently removed e.g. by centrifugal separation. Since the resulting degummed oil often still contains unacceptably high levels of 'non-hydratable' phos-phatldes, this water~degumming step is normally followed bychemical treatments with acid and/or alkali to remove the ~20307 residual phosphatides and to neutralize the free fatty acids (~alkali-refining~). Subsequently, the soapstock so formed is separated from the neutrali~ed oil by centrifugal separa-tion.
Soapstock containing the afore-mentioned non-triglyceride components and has to be split prior to it's disposal in order to recover the fatty acids contained therein, and to obtain an effluent (acid water) containing low levels of total fatty matter (TFM), that is material lo soluble in ether.
During the splitting of the soapstock using a soap splitting acid, such as sulphuric acid, at pH 2 and a soap splitting temperature of 95C, an emulsion may be formed.
The emulsion formation occurs especially when splitting maize- or sunflower soapstock.
There are several unit operations available to break the emulsions formed. These unlt operations comprise filtra-tion, centrifugation, settling during long time periods and a low pH treatment. All these unit operation are cumbersome, because of the corrosive nature of the emulsion (for instance a pH of 4 or lower), whereas due to the large amount of acid used the effluent may require a pre-treatment before disposal.
NL-A-69 17290 discloses a method and an apparatus for continuously splitting of soapstock formed in the alkall reflning of crude glyceride oil, in which an inorganic acld is lntensively mixed with steam ln a Venturl tube, and subsequently the acid steam mlxture is lntensively mlxed wlth soapstock ln a second Venturl tube. The soapstock had a temperature of 80-95C and was passed through a separatlon zone comprising a packed bed of filling material.
GB-A-1,307,862 discloses a process for treating a solutlon comprlslng soapstock, sulphonate salt and an lnorganlc salt for the recovery of fatty acid and a sulphonate salt solution therefrom. This mixture is acidified at 80C to pH 2,5 using sulphoric acid.
US-A-4,118,407 discloses a process for recovering free fatty acid from aqueous crude soapstock containing ~3~ 2020307 saponlfiable fatty material comprising a glyce~ide oil, comprising a saponification zone in which crude soapstock is mixed with an inorganic base and recycled inorganic salt containing neutralized acid water. The saponified soapstock is passed to a acidulation zone in which it is mixed with an inorganic salt at a temperature of between about 80-95C.
Finally, a free fatty acid stream is separated in a separation zone and neutralized acid water is recycled to the saponification zone.
US-A-4,671,902 discloses a method for the preparation of fatty acid products from glyceride oil soapstock, in which the soapstock is acidulated with an aqueous mineral acid, and after separation of an aqueous solution the remaining emulsion of fatty material and sludge is dried to a watter content of less than 5% resulting in a breakage of the emulsion. The acidiflcation is carried out at 80-95C, at a pH of 3-4, for at least two hours.
It has been found that when the mixture of soapstock and soap splitting agent is sub;ected to a high temperature treatment, the emulsion formation is substantially avoided.
Accordingly, an ob;ect of the invention is to provide a process for splitting soapstock, by which the emulsion formatlon is substantially avoided and accordingly, the acid water phase and oll phase formed are easily separatable from one another. The process of the invention is characterized in that the mixture of the soapstock and the soap splitting acid are sub~ected to a high temperature treatment at or above 100C during a residence tlme equal to or more than 2 minutes.
Preferably the high temperature treatment ls carried out at a temperature of about 100-150C. The upper temperature limit is elected such that the pressure is not too far above atmospheric pressure (pressure less than 6 bar).
Generally, a residence time of about 15-60 minutes is sufficient and optimal results are obtained after a resi-dence time of about 20-40 minutes.
-q- 2020307 Generally, the high temperature treatment is carried out at a pH of about 0~5-4, particularly at a pH near or equal to pTI 2.
Preferably, the splitted soapstock is settled at a temperature lower than the temperature of the high temperature treatment for separating the acid oil phase from the acid water phase. Preferably, the settling is carried out after cooling to a temperature of about 50-95C. A lower settling temperature is preferred, because at those lower temperatures the phase separation occurs within normally 15 minutes and the decrease of the solubility of the total fatty matter (TFM) in the acid water phase is larger than the increase of the viscosity of water.Finally, settling at the high temperature requires a pressure vessel, cooling of the acid water outlet and high investment costs for the pressure settling vessel and above all severe corrosion problems.
Generally, the high temperature treatment according to the invention leads to significantly lower TFM contents in the acid water phase, generally to TFM contents less than lO00 ppm.
Preferably, the soapstock originates from non-degummed or water-degummed glyceride oil.
The soap splitting process according to the invention may be used in a continuous process or in a batchwise process.
The following examples are given to illustrate the soap splitting process according to the invention, and may not be construed as to limit the invention described herein.
EXAMPLE I
Soapstock originating from non-degummed maize oil heated to a temperature of 95C was mixed with concentrated sulphuric acid untill pH 2 was reached. The mixture of soapstock and sulphuric acid was subjected to the high temperature treatment accordlng to the invention, using temperatures indicated in table l, and allowing a residence time of 2 minutes. The amount of TFM in the acid water phase was
2~0307 compared to the amount present in the acid water phase obtained under prior art soap splitting conditions (temperature 95C; residence time 2 minutes).
Table 1 _ _ T ( C)TFM ~*1000 ppm) 44.0 110 11 . O
125 3.9 130 1.2 15 150 0.8 . . . _ _ EXAMPLE I I
Soapstock originating from non-degummed maize oil and non-degummed sunflower oil was split at pH 2 using sulphuric acid, whereafter the splitted soapstock was allowed a resi-dence time of 2 minutes at 95C (prior art) or at 150C
~according to the invention). Settling was carried out at 95C for 1 hour.
The TFM contents of the acid water obtained are listed in table 2.
Table 2 . .
TFM content acid water (ppm) after 2 minutes at ____________________________ Soapstock 95C 150C
maize 44,000 800 sunflower 12,40Q 420 EXAMPLE I I I
Soapstock originating from non-degummed maize oil was soap splitted at pH 2 using sulphuric acid. Thereafter the splitted soap stock was sub;ected to the high temperature treatment at 150C during various residence times indicated in table 3. Settling was carried out at 95C for 1 hour.
The TFM contents of the acid water obtained are also indicated in table 3.
Table 3 residence TFM
time (min~ (ppm) _ EXAMPLE IV
Soapstock origlnatlng from sunflower oil having a high con-tent of partially unsaturated fatty acids was soap splitted in a continuous process at 95C and pH 2. Without the high temperature treatment according to the invention the aqueous phase contalned 49,700 ppm TFM, and after the hlgh tempera-ture treatment accordlng to the invention at 130C and 150C
were 750 and 250 ppm TFM, respectively.
EXAMPLE V
Soapstock originating from water-degummed malze oll was sub-~ected to soap spllttlng uslng sulphuric acid at 95C and pH
2. Without the high temperature treatment according to the invention the aqueous phase comprised 8040 ppm TFM. After the high temperature treatment according to the lnvention at 140C and a residence time of 20 and 30 minutes the TFM
content of the acid water phase decreased to 170 and 260 ppm TFM, respectively.
*****
Table 1 _ _ T ( C)TFM ~*1000 ppm) 44.0 110 11 . O
125 3.9 130 1.2 15 150 0.8 . . . _ _ EXAMPLE I I
Soapstock originating from non-degummed maize oil and non-degummed sunflower oil was split at pH 2 using sulphuric acid, whereafter the splitted soapstock was allowed a resi-dence time of 2 minutes at 95C (prior art) or at 150C
~according to the invention). Settling was carried out at 95C for 1 hour.
The TFM contents of the acid water obtained are listed in table 2.
Table 2 . .
TFM content acid water (ppm) after 2 minutes at ____________________________ Soapstock 95C 150C
maize 44,000 800 sunflower 12,40Q 420 EXAMPLE I I I
Soapstock originating from non-degummed maize oil was soap splitted at pH 2 using sulphuric acid. Thereafter the splitted soap stock was sub;ected to the high temperature treatment at 150C during various residence times indicated in table 3. Settling was carried out at 95C for 1 hour.
The TFM contents of the acid water obtained are also indicated in table 3.
Table 3 residence TFM
time (min~ (ppm) _ EXAMPLE IV
Soapstock origlnatlng from sunflower oil having a high con-tent of partially unsaturated fatty acids was soap splitted in a continuous process at 95C and pH 2. Without the high temperature treatment according to the invention the aqueous phase contalned 49,700 ppm TFM, and after the hlgh tempera-ture treatment accordlng to the invention at 130C and 150C
were 750 and 250 ppm TFM, respectively.
EXAMPLE V
Soapstock originating from water-degummed malze oll was sub-~ected to soap spllttlng uslng sulphuric acid at 95C and pH
2. Without the high temperature treatment according to the invention the aqueous phase comprised 8040 ppm TFM. After the high temperature treatment according to the lnvention at 140C and a residence time of 20 and 30 minutes the TFM
content of the acid water phase decreased to 170 and 260 ppm TFM, respectively.
*****
Claims (9)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. Process for splitting soapstock, comprising the steps of mixing the soapstock with a soap splitting acid, and of separating the acid water phase formed from the oil phase, characterized in that the mixture of the soapstock and the soap splitting agent are subjected to a high tempe-rature treatment at or above 100°C during a residence time equal to or more than 2 minutes.
2. Process as claimed in claim 1, wherein the high temperature treatment is carried out at a temperature of about 100-150°C.
3. Process as claimed in claim 1 or 2, wherein the residence time is about 15-60 minutes.
4. Process as claimed in claim 3, wherein the resi-dence time is about 20-40 minutes.
s. Process as claimed in claim 1-4, wherein the high temperature treatment is carried out at a pH of about 0.5-4.
6. Process as claimed in claim 1-5, wherein after the high temperature treatment the mixture is cooled to a tempe-rature below about 100°C, and allowed to settle.
7. Process as claimed in claim 6, wherein the mixture is cooled to a temperature of about 50-95°C.
8. Process as claimed in claim 6 or 7, wherein the settling time period is about 30-120 minutes.
9. Process as claimed in claim 1-8, wherein the water phase separated has a total fatty matter (TFM) content of less than 1000 ppm.
*****
*****
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB8915263A GB8915263D0 (en) | 1989-07-03 | 1989-07-03 | Process for soap splitting using a high temperature treatment |
| GB89.15263.1 | 1989-07-03 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2020307A1 true CA2020307A1 (en) | 1991-01-04 |
Family
ID=10659480
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002020307A Abandoned CA2020307A1 (en) | 1989-07-03 | 1990-07-03 | Process for soap splitting using a high temperature treatment |
Country Status (14)
| Country | Link |
|---|---|
| US (1) | US5210242A (en) |
| EP (1) | EP0406945B1 (en) |
| JP (1) | JPH0354299A (en) |
| AT (1) | ATE131205T1 (en) |
| AU (1) | AU631891B2 (en) |
| CA (1) | CA2020307A1 (en) |
| CS (1) | CS277234B6 (en) |
| DD (1) | DD296306A5 (en) |
| DE (1) | DE69023968T2 (en) |
| DK (1) | DK0406945T3 (en) |
| ES (1) | ES2081908T3 (en) |
| GB (1) | GB8915263D0 (en) |
| HU (1) | HU205970B (en) |
| ZA (1) | ZA905052B (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FI93868C (en) * | 1990-12-28 | 1995-06-12 | Veitsiluoto Oy | Manufacture of tall oil |
| JP5381676B2 (en) * | 2009-12-14 | 2014-01-08 | 株式会社大林組 | Surface finishing method |
| WO2016149692A1 (en) | 2015-03-19 | 2016-09-22 | Inventure Renewables, Inc. | Complete saponification and acidulation of natural oil processing byproducts and treatment of reaction products |
| US11549081B2 (en) * | 2016-04-18 | 2023-01-10 | Rrip, Llc | Method to destabilize emulsion feedstocks for the recovery of valuable products |
| FI128345B (en) | 2016-08-05 | 2020-03-31 | Neste Oyj | Process for purifying a feedstock |
| US9745541B1 (en) | 2016-09-09 | 2017-08-29 | Inventure Renewables, Inc. | Methods for making free fatty acids from soaps using thermal hydrolysis followed by acidification |
| EP3877355A4 (en) | 2018-11-06 | 2022-08-03 | Inventure International (Pte) Limited | Methods for making free fatty acids and fatty acid derivatives from mixed lipid feedstocks or soapstocks |
Family Cites Families (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE541015A (en) * | ||||
| US3428660A (en) * | 1964-01-20 | 1969-02-18 | Baker Perkins Inc | Process for recovering fatty acids and triglyceride oil from soapstock |
| US3525938A (en) * | 1966-10-31 | 1970-08-25 | Westinghouse Electric Corp | Static frequency meter |
| US3425938A (en) * | 1967-06-09 | 1969-02-04 | Arkansas Grain Corp | Soapstock acidulation |
| US3787460A (en) * | 1968-12-17 | 1974-01-22 | Lever Brothers Ltd | Process for splitting soapstock and apparatus therefor |
| GB1307862A (en) * | 1970-05-07 | 1973-02-21 | Albright & Wilson | Fatty acid recovery process |
| JPS49124103A (en) * | 1973-03-31 | 1974-11-27 | ||
| GB1559794A (en) * | 1975-09-04 | 1980-01-30 | Unilever Ltd | Continuous soapstock splipping |
| US4118407A (en) * | 1977-01-06 | 1978-10-03 | Scm Corporation | Fatty acid recovery from soapstock |
| JPS58103597A (en) * | 1981-12-16 | 1983-06-20 | 日清製油株式会社 | Crude fatty acid continuous manufacture |
| US4464305A (en) * | 1982-09-23 | 1984-08-07 | Patrick Jr Charles H | Process for the recovery of fatty acids from discarded solid soap materials |
| EP0174938B1 (en) * | 1984-01-18 | 1990-11-28 | DANIELS, Ralph S. | Fertilizer process |
| US4671902A (en) * | 1984-03-12 | 1987-06-09 | The Procter & Gamble Company | Process for obtaining fatty acid product from glyceride oil soapstock |
-
1989
- 1989-07-03 GB GB8915263A patent/GB8915263D0/en active Pending
-
1990
- 1990-06-26 AU AU57828/90A patent/AU631891B2/en not_active Ceased
- 1990-06-27 ES ES90201708T patent/ES2081908T3/en not_active Expired - Lifetime
- 1990-06-27 DK DK90201708T patent/DK0406945T3/en active
- 1990-06-27 DE DE69023968T patent/DE69023968T2/en not_active Expired - Fee Related
- 1990-06-27 EP EP19900201708 patent/EP0406945B1/en not_active Revoked
- 1990-06-27 AT AT90201708T patent/ATE131205T1/en not_active IP Right Cessation
- 1990-06-28 US US07/546,158 patent/US5210242A/en not_active Expired - Fee Related
- 1990-06-28 ZA ZA905052A patent/ZA905052B/en unknown
- 1990-06-28 CS CS903225A patent/CS277234B6/en unknown
- 1990-06-29 JP JP2172556A patent/JPH0354299A/en active Pending
- 1990-07-02 DD DD90342437A patent/DD296306A5/en not_active IP Right Cessation
- 1990-07-02 HU HU904060A patent/HU205970B/en not_active IP Right Cessation
- 1990-07-03 CA CA002020307A patent/CA2020307A1/en not_active Abandoned
Also Published As
| Publication number | Publication date |
|---|---|
| HU205970B (en) | 1992-07-28 |
| AU5782890A (en) | 1991-01-03 |
| HU904060D0 (en) | 1990-12-28 |
| CS277234B6 (en) | 1992-12-16 |
| AU631891B2 (en) | 1992-12-10 |
| DE69023968T2 (en) | 1996-05-23 |
| DK0406945T3 (en) | 1996-04-09 |
| EP0406945B1 (en) | 1995-12-06 |
| DD296306A5 (en) | 1991-11-28 |
| ATE131205T1 (en) | 1995-12-15 |
| GB8915263D0 (en) | 1989-08-23 |
| US5210242A (en) | 1993-05-11 |
| ES2081908T3 (en) | 1996-03-16 |
| EP0406945A2 (en) | 1991-01-09 |
| HUT56390A (en) | 1991-08-28 |
| JPH0354299A (en) | 1991-03-08 |
| ZA905052B (en) | 1992-02-26 |
| DE69023968D1 (en) | 1996-01-18 |
| CS322590A3 (en) | 1992-04-15 |
| EP0406945A3 (en) | 1992-01-08 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| FZDE | Discontinued |